CN217698338U - Yellow phosphorus furnace gas dry method dust collector - Google Patents

Abstract

The utility model relates to a yellow phosphorus furnace gas dry method dust removal device, relating to the field of furnace gas purification and dust removal, in particular to a yellow phosphorus furnace gas dry method dust removal device, which comprises a dust remover body, wherein the dust remover body comprises an upper cylinder, a middle cone and an ash bucket; the upper cylinder is communicated with an ash bucket through a middle cone, and the lower end of the ash bucket is connected with an ash discharge pipe through an ash discharge valve; a cylinder exhaust pipe is arranged at the center of the top of the upper cylinder, and an inlet pipe is also arranged at the upper end of the upper cylinder; the utility model has no other internal parts in the upper cylinder and the middle cone, so the resistance is lower, and tar adhesion can not be caused. The utility model discloses set up steam jacket and utilize the high temperature steam of mill's self-production to give dust remover casing heat tracing, do not have the liquid yellow phosphorus that the condensation got off in the ash bucket, even if consequently arrange grey in-process contact air can not take place yellow phosphorus spontaneous combustion yet to the corresponding improvement of product yellow phosphorus yield.

Description

Yellow phosphorus furnace gas dry method dust collector

Technical Field

The utility model relates to a kiln gas purifies dust removal field, concretely relates to yellow phosphorus stove gas dry process dust collector.

Background

China yellow phosphorus production enterprises mainly concentrate on Yuxi, chengjiang and Jingqu in Yunnan, open Yang, van An and Fuquan in Guizhou, and areas such as Rabobo in Sichuan, horse side and the like, and the yellow phosphorus production capacity of the Yuntai province accounts for about 90% of the total yellow phosphorus production capacity in China. The CO content in high-temperature furnace gas discharged from a yellow phosphorus electric furnace accounts for 80 to 90 percent, and the content of gaseous elemental phosphorus accounts for 300 to 350g/m³40 to 120g/m of dust³Simultaneously contains a certain amount of HF and SiF₄、H₂S、COS、PH₃、AsH₃And harmful impurities such as HCN and tar. Yellow phosphorus plants in Guizhou and Sichuan basically adopt anthracite (white coal) as a reducing agent, most yellow phosphorus plants in Yunnan adopt coke (coke) as the reducing agent, the content of dust and tar in phosphorus furnace gas adopting the anthracite as the reducing agent is higher, and H is higher₂The S and COS contents are high.

The electric furnaces generally adopted in the yellow phosphorus industry in China are basically medium-sized or small-sized electric furnaces, the temperature of a phosphorus furnace at the outlet of the furnace top is generally 130 to 200 ℃, and the temperature of furnace gas can reach more than 280 ℃ under abnormal working conditions. The high-temperature furnace gas in production enters a 3-4 grade spray phosphorus cooling tower through a gas guide pipe to finish condensation and recovery of gaseous phosphorus, and the furnace gas is purified to a certain degree. In the process of spraying and cooling the phosphorus furnace gas, dust and harmful impurities in the furnace gas are absorbed, adhered and trapped into a phosphorus receiving groove at the bottom of the tower by liquid drops, and SiF₄Hydrolyzing to obtain fluosilicic acid precipitate, wrapping dust, fluosilicic acid, tar, etc. with yellow phosphorus to form phosphorus mud colloid, and performing primary settling separation of crude yellow phosphorus and phosphorus mud by density difference, and further rinsing and refining to obtain yellow phosphorus product. Therefore, a large amount of phosphorus mud is generated in the production of yellow phosphorus, the phosphorus mud needs to be subjected to rotary pan drying and phosphorus steaming treatment to reduce the phosphorus content in the phosphorus mud, and the phosphorus mud after phosphorus steaming is comprehensively utilized.

Because the amount of dust in the furnace gas is large, the amount of phosphorus mud generated in the traditional production operation process is large, if most of dust in the furnace gas can be removed before spraying and washing, the generation amount of the phosphorus mud can be obviously reduced, the sedimentation separation of the crude yellow phosphorus and phosphorus mud colloidal substances becomes easy, the purity of the crude yellow phosphorus can be improved to more than 85%, the rinsing, refining and separating process of the rear-end crude yellow phosphorus is easier due to the crude yellow phosphorus with higher purity, and the rinsing, sedimentation and separating time is greatly shortened. Meanwhile, the rear-end phosphorus mud treatment capacity is obviously reduced. On the other hand, because the dust content of furnace gas entering the spray cooling phosphorus system is obviously reduced, the mud content in the circulating spray water is correspondingly reduced, the using amount of the water treatment flocculating agent is reduced, the circulating water quality is improved, and the spray washing process is facilitated. From the energy-saving perspective, the dry dust obtained by dry dedusting does not need drying treatment, the drying fuel is saved, the phosphorus mud amount is reduced by 60 to 70 percent, and the steam consumption in the process of rinsing and refining the crude phosphorus is reduced.

In China, yellow phosphorus production enterprises try to remove dust by a dry method, for example, electrostatic dust removal, cloth bag dust removal and other filtering dust removal are adopted, but the dry dust removal and the cloth bag dust removal are not successfully applied, only the electrostatic dust remover is successfully applied to the dust removal of furnace gas of a large-scale electric furnace, and two sets of electrostatic dust removers are adopted, one set is used, the other set is prepared, and the using period is switched for about 10 to 14 days. The design dust removal efficiency of the electrostatic dust collector is 99%, and the actual dust removal efficiency is 70-80% from the operating condition of the electrostatic dust collector in a large electric furnace.

Although the electrostatic dust collector is successfully applied to a large electric furnace, the electrostatic dust collector cannot be successfully used in medium and small electric furnaces widely adopted by yellow phosphorus factories in China, the fundamental reason is the difference of production processes of the large electric furnace and the medium and small electric furnaces, the furnace gas temperature of the large electric furnace is about 350 to 500 ℃, the furnace gas temperature of the medium and small electric furnaces is generally less than 200 ℃, compared with the large electric furnace, the furnace gas temperature of the medium and small electric furnaces is lower, phosphorus vapor in the furnace gas is easy to condense on the surface of a settling grade, tar in the furnace gas can also adhere to the settling grade, and the defect which cannot be overcome in the production process is caused. In addition, the two sets of electrostatic dust collectors are high in investment cost, a large amount of high-temperature nitrogen is needed to keep the temperature of the shell of the electrostatic dust collector in the operation process, most enterprises are not provided with air separation devices and do not have sufficient nitrogen sources, in addition, the power consumption is increased by adopting electric heating nitrogen, and the unit consumption of yellow phosphorus products is correspondingly increased.

The bag type dust collector has been subjected to dust collection tests on small and medium-sized electric furnaces, and has the similar problems with the electrostatic dust collector, because an inner cloth bag cannot be provided with heat insulation, phosphorus vapor is condensed, and tar adheres to the cloth bag and cannot be cleaned to stop operation. In addition, the temperature of furnace gas can reach over 280 ℃ when the electric furnace is not normally operated, and the cloth bag is easy to burn out.

The dry dedusting of the yellow phosphorus furnace gas has great technical difficulty and more potential safety hazards, for example, the phosphorus furnace gas is flammable and explosive, and has CO poisoning, the furnace gas contains adhesive tar, a large amount of phosphorus vapor is easy to condense into liquid yellow phosphorus, and the yellow phosphorus is subjected to spontaneous combustion in the air. Therefore, the dry dust removal of the yellow phosphorus furnace gas is more difficult than dust removal of coke oven gas, blast furnace gas, ore kiln gas and the like, and the safety design of the dust removal process needs to be considered in an important way.

At present, dry dust removal is not generally arranged on middle and small-sized electric furnaces in China, and yellow phosphorus production enterprises need a dry dust removal device which can be successfully applied to yellow phosphorus furnace gas, so that a safe, reliable and efficient yellow phosphorus furnace gas dry dust removal device is urgently needed to be developed.

SUMMERY OF THE UTILITY MODEL

In order to solve the problem, the utility model provides a yellow phosphorus furnace gas dry method dust collector which reduces the dust disturbance and improves the dust removal efficiency.

The utility model relates to a gas dry dust removal device of a yellow phosphorus furnace, which comprises a dust remover body, wherein the dust remover body comprises an upper barrel, a middle cone and an ash bucket; the upper cylinder is communicated with an ash bucket through a middle cone, and the lower end of the ash bucket is connected with an ash discharge pipe through an ash discharge valve;

a barrel exhaust pipe is arranged at the center of the top of the upper barrel, one end of the barrel exhaust pipe is positioned in the upper barrel, the other end of the barrel exhaust pipe extends out of the upper barrel, an inlet pipe is further arranged at the upper end of the upper barrel, the inlet pipe is arranged in a tangent manner with the outer wall of the upper barrel, the inlet pipe extends towards one end of the upper barrel and is arranged obliquely downwards, and the bottom of the inlet pipe is flush with one end of the barrel exhaust pipe, which is positioned in the upper barrel;

the connecting part of the middle cone and the ash bucket is also provided with a double cone, the double cone comprises an upper cone and a lower cone which are frustum-shaped, the small end surface of the upper cone is fixedly connected with the small end surface of the lower cone, and the minimum section at the necking part of the double cone is positioned on the same plane with the connecting plane of the middle cone and the ash bucket; an airflow channel for communicating the middle cone and the ash bucket is arranged in the double cones, the central axes of the double cones and the central axis of the upper barrel are positioned on the same straight line, and the lower parts of the double cones are fixedly connected with the inner wall of the ash bucket through connecting strips;

the steam humidifying device is arranged on the outer peripheral surfaces of the upper barrel and the middle cone;

the steam humidifying pipeline is connected with a steam humidifying and atomizing nozzle through a steam valve, and the steam humidifying and atomizing nozzle is arranged in the inlet pipe;

a temperature and humidity sensor is fixedly arranged in the cylinder exhaust pipe and is in linkage with the steam valve.

Preferably, the angle of inclination of the inlet pipe is α, α being 10 to 16 °.

Preferably, the cross section of the inlet pipe is rectangular, and the inclination angle of the inlet pipe is α satisfying tan α =0.5A/D, where a is the opening width of the inlet pipe in the vertical direction and D is the diameter of the upper cylinder.

Preferably, still include the nitrogen gas intake pipe, the nitrogen gas intake pipe is connected with the nitrogen gas nozzle through the nitrogen gas valve, the nitrogen gas nozzle is fixed to be set up in the ash discharge pipe, the internal fixed oxygen content monitoring sensor that is provided with of middle part awl, oxygen content monitoring sensor and nitrogen gas nozzle linkage set up.

Preferably, a material level meter is arranged in the ash hopper, and the material level meter is in linkage with the ash discharge valve.

Preferably, the cylinder exhaust pipe is a gradually-expanding cylinder exhaust pipe, and the expansion angle is 6-15 degrees.

Or preferably, the heating device is a steam jacket which is sleeved outside the upper cylinder and the middle cone and is communicated with each other, the upper part of the steam jacket is provided with a steam inlet, and the lower part of the steam jacket is provided with a condensed water outlet.

The utility model discloses utilize the centrifugal dust remover that centrifugal separation principle designed, there are not other internals in upper portion barrel and the middle cone, therefore the resistance falls lowly, and can not cause the tar adhesion.

The utility model discloses set up steam jacket and utilize the high temperature steam of mill's self-production to give dust remover casing companion's heat, when saturated steam temperature more than 180 ℃, correspond saturated vapor pressure 1.0MPa, then the phosphorus vapour in the phosphorus burner gas is in the utility model discloses the volume of condensing is very little on the inner wall, does not basically have the liquid yellow phosphorus that the condensation got off in the ash bucket, even if consequently arrange grey in-process contact air can not take place yellow phosphorus spontaneous combustion yet to the corresponding improvement of product yellow phosphorus yield. Similarly, the tar gas in the phosphorus furnace gas is in the utility model discloses the volume that the inner wall took place the condensation is also few, and tar is under high temperature companion's hot state moreover, and viscosity is lower can not the utility model discloses the inner wall produces the adhesion.

The centrifugal dust remover has high dust removal rate for the particle size of more than 5 mu m and low removal rate for the fine dust with the particle size of less than 3 mu m. The utility model discloses set up the steam humidification nozzle at the entry, carried out the humidification to dry phosphorus stove gas with saturated steam, set up temperature and humidity sensor in the dust remover export, the steam valve linkage on temperature and humidity sensor and the steam humidification pipeline is in order to control the aperture of steam valve, and the phosphorus stove gas phase after the humidification maintains 50 to 60% to humidity. Because the relative humidity of the phosphorus furnace gas is increased, fine dust in the furnace gas is easy to combine into dust with larger particle size in the high-speed rotational flow process, and is thrown to the wall of the furnace by centrifugal force to be captured, so the utility model discloses can improve to 50 to 60% from 20 to 30% to the clearance of fine dust.

The inclination angle alpha of the inlet pipe is 10-16 degrees, preferably, tan alpha =0.5A/D is satisfied, A is the height of the inlet rectangle, and D is the diameter of the cylinder. The design has the advantages that no turbulent flow occurs between each circle of air flow with the inner wall of the dust remover spirally downward, the disturbance of the dust on the wall of the dust remover is reduced, and the space of the dust remover is utilized to the maximum extent, so that the improvement of the dust removal efficiency is facilitated. The central exhaust pipe at the upper end of the dust remover is designed into an expanding pipe, the expansion angle is 6 to 15 degrees by utilizing the speed reduction and pressure expansion principle, and the outlet resistance of the dust remover is reduced by about 30 percent compared with a straight-barrel type exhaust pipe.

The lower end of the middle cone is connected with the lower ash bucket, and a double cone is arranged in the center of the inner part of the middle cone. In the process that dust falls along the wall of a vessel, the lower end of the middle cone body can hoist a small amount of dust at the lower end of the middle cone body and in the dust hopper again due to the return turbulent flow of air flow, secondary dust raising is caused, the dust removal efficiency is reduced, and the problem of secondary dust raising is solved and the resistance of the dust remover cannot be increased due to the ingenious design of the double cone body. Dust on the dust remover inner wall falls into the ash bucket in the annular space between the bipyramid that middle part cone lower extreme and inside center set up, and most air current is inverting the bipyramid top and is turning back the entering the utility model discloses the center, the secondary raise dust that the air current that has turned back arouses has effectively been solved in this design. A small part of air flow enters the lower ash bucket along with dust from the annular gap, and returns back to enter the double cones at the center of the ash bucket in the ash bucket, the air flow in the ash bucket discharges out of the double cones, the flow speed is reduced and the pressure rises back in the upper cone, so that the rising pressure of the air flow is improved, and the air flow is discharged conveniently. Because the upper end of the center of the ash bucket is provided with the double cones, the dust falling into the ash bucket is distributed in a shallow V shape, the dust falling from the annular gap is mainly concentrated at the position close to the wall surface of the ash bucket, the position of the dust close to the center of the ash bucket is lower and is not easily brought out by the airflow, and the turning angle of the airflow is reduced from 170 degrees to about 140 degrees, so that the dust brought out by the airflow in the ash bucket is obviously reduced, and the dust brought out is further reduced by the design of the lower cones.

The utility model discloses a charge level indicator sets up with the linkage of ash valve, and when the material level was less than 12cm in the ash bucket, the ash valve stopped the ash discharge, kept the material level height in the ash bucket to be not less than 10cm.

The utility model discloses a solid cone type nozzle, preferred venturi injection formula nozzle can be chooseed for use to the nitrogen gas nozzle. The utility model discloses middle part cone center sets up oxygen content monitoring sensor, and the nitrogen valve linkage on this oxygen content monitoring sensor and the nitrogen gas jetting pipe, when the oxygen content of monitoring is higher than 1.0%, opens the nitrogen valve voluntarily, prevents that the air from leaking into the dust remover.

The utility model discloses heating device can adopt steam heating, also can adopt the high temperature flue gas heating that yellow phosphorus tail gas burning produced, needs to establish the flue gas draught fan in addition.

The ash discharge pipe of the utility model can be inserted into the ash groove to obtain dry ash; the mortar discharge pipe can also be inserted below the water surface to obtain mortar, and a filter system is additionally arranged to dehydrate the mortar.

The utility model provides a safe and reliable and efficient yellow phosphorus stove gas dry process dust collector has not only solved the difficult point that middle-size and small-size yellow phosphorus stove gas dry process removed dust, and the dry process dust collector dust collection efficiency of design can reach 92%.

The utility model discloses the investment is low, is 60% of the used electrostatic precipitator investment cost of large-scale electric stove under the same handling capacity, and the device diameter is little, and occupation of land is little, is convenient for reform transform on the spot near the electric stove.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

Reference numerals: the system comprises a temperature and humidity sensor 1, a steam valve 2, a steam humidifying and atomizing nozzle 3, an inlet pipe 4, an oxygen content monitoring sensor 5, a nitrogen valve 6, a nitrogen nozzle 7, an ash discharge valve 8, a charge level indicator 9, a double cone 10, a condensate water outlet 11, a middle cone 12, an upper barrel 13, a steam inlet 15 and a steam jacket 16.

Detailed Description

The utility model relates to a gas dry dust removal device of a yellow phosphorus furnace, which comprises a dust remover body, wherein the dust remover body comprises an upper barrel 13, a middle cone 12 and an ash bucket; the upper cylinder 13 is communicated with an ash bucket through a middle cone 12, and the lower end of the ash bucket is connected with an ash discharge pipe through an ash discharge valve 8;

a barrel exhaust pipe is arranged at the center of the top of the upper barrel 13, one end of the barrel exhaust pipe is positioned in the upper barrel 13, the other end of the barrel exhaust pipe extends out of the upper barrel 13, an inlet pipe 4 is further arranged at the upper end of the upper barrel 13, the inlet pipe 4 is arranged in a tangent manner with the outer wall of the upper barrel 13, one end of the inlet pipe 4 extending towards the upper barrel 13 is arranged in an inclined and downward manner and is flush with one end of the barrel exhaust pipe positioned in the upper barrel 13, namely the bottom of one end of the inlet pipe extending into the upper barrel 13 is flush with one end of the barrel exhaust pipe positioned in the upper barrel 13;

a double cone 10 is further arranged at the joint of the middle cone 12 and the ash bucket, the double cone 10 comprises an upper cone and a lower cone which are in frustum shapes, the small end face of the upper cone is fixedly connected with the small end face of the lower cone, and the minimum section of the necking position of the double cone 10 is positioned on the same plane as the joint plane of the middle cone 12 and the ash bucket; an airflow channel for communicating the middle cone 12 and the ash bucket is arranged in the double cone 10, the central axis of the double cone 10 and the central axis of the upper cylinder 13 are positioned on the same straight line, and the lower part of the double cone 10 is fixedly connected with the inner wall of the ash bucket through a connecting strip;

the steam humidification device further comprises a heating device and a steam humidification pipeline, wherein the heating device is arranged on the outer peripheral surfaces of the upper barrel 13 and the middle cone 12;

the steam humidifying pipeline is connected with a steam humidifying and atomizing nozzle 3 through a steam valve 2, and the steam humidifying and atomizing nozzle 3 is arranged in an inlet pipe 4;

a temperature and humidity sensor 1 is fixedly arranged in the cylinder exhaust pipe, and the temperature and humidity sensor 1 and the steam valve 2 are arranged in a linkage mode.

The inclination angle of the inlet pipe 4 is alpha, and alpha is 10 to 16 degrees.

The cross section of the inlet pipe 4 is rectangular, and the inclination angle of the inlet pipe 4 is α so as to satisfy tan α =0.5A/D, where a is the opening width of the inlet pipe 4 in the vertical direction, and D is the diameter of the upper cylinder 13.

Still include the nitrogen gas intake pipe, the nitrogen gas intake pipe is connected with nitrogen gas nozzle 7 through nitrogen gas valve 6, nitrogen gas nozzle 7 is fixed to be set up in the ash discharge pipe, the internal fixation of middle part cone 12 is provided with oxygen content monitoring sensor 5, oxygen content monitoring sensor 5 sets up with the linkage of nitrogen gas nozzle 7.

A material level meter 9 is arranged in the ash bucket, and the material level meter 9 and the ash discharge valve 8 are arranged in a linkage manner.

The cylinder exhaust pipe is a gradually-expanded cylinder exhaust pipe, and the expansion angle is 6-15 degrees.

The heating device is a steam jacket 16 which is sleeved outside the upper cylinder 13 and the middle cone 12 and is communicated with each other, a steam inlet 15 is arranged at the upper part of the steam jacket 16, and a condensed water outlet 11 is arranged at the lower part of the steam jacket 16.

3760Nm 3/ml & lt/EN & gt of phosphorus furnace gas treatment capacity of certain yellow phosphorus factory in Yunnanh, according to the utility model discloses corresponding one set of phosphorus burner gas dust collector of having designed, concrete design parameter is as follows:

throughput of treatment	3760Nm3/h	Steam jacket design pressure	1.5MPa
				Mean temperature	170℃	Height of cylinder	1.5m
Actual flow rate	6100m3/h	Height of cone	1.8m
				Inlet gas velocity	16m/s	Vertex angle of cone	17.0°
Height of entrance	0.5m	Double cone upper apex angle	17.0°
				Width of entrance	0.22m	Height of upper end of bicone	0.34m
Diameter of cylinder	0.9m	Double cone lower end vertex angle	20.0°
				Inlet pipe inclination angle	15.5°	Height of lower end of bicone	0.4m
Diameter of outlet	0.42m	Diameter of ash bucket	0.8m
				Diameter of dust exhaust port	0.36m	Height of ash bucket	1.0m
Depth of insertion of barrel exhaust pipe	0.5m	Top angle of lower cone of ash bucket	32°

The dust removal device is used for pretreating the dust of the phosphorus furnace gas, the operation is stable, and the average dust concentration at the inlet of the dust removal device in a certain period is 78.52g/m³The dust concentration at the outlet of the dust collector is 5.91 g/m³The dust removal efficiency is 92.4%, and the dust removal effect is good.

Claims (7)

1. A yellow phosphorus furnace gas dry dust removal device comprises a dust remover body, wherein the dust remover body comprises an upper cylinder (13), a middle cone (12) and an ash bucket; the device is characterized in that the upper cylinder (13) is communicated with an ash bucket through a middle cone (12), and the lower end of the ash bucket is connected with an ash discharge pipe through an ash discharge valve (8);

a barrel exhaust pipe is arranged at the center of the top of the upper barrel (13), one end of the barrel exhaust pipe is positioned in the upper barrel (13), the other end of the barrel exhaust pipe extends out of the upper barrel (13), an inlet pipe (4) is further arranged at the upper end of the upper barrel (13), the inlet pipe (4) is arranged in a tangent mode with the outer wall of the upper barrel (13), one end of the inlet pipe (4) extending to the upper barrel (13) is arranged in an inclined mode downwards, and the bottom of the inlet pipe is flush with one end, positioned in the upper barrel (13), of the barrel exhaust pipe;

a double cone (10) is further arranged at the joint of the middle cone (12) and the ash bucket, the double cone (10) comprises an upper cone and a lower cone which are frustum-shaped, the small end face of the upper cone is fixedly connected with the small end face of the lower cone, and the minimum section of the necking part of the double cone (10) is positioned on the same plane as the joint plane of the middle cone (12) and the ash bucket; an airflow channel for communicating the middle cone (12) and the ash bucket is arranged in the double cone (10), the central axis of the double cone (10) and the central axis of the upper cylinder (13) are positioned on the same straight line, and the lower part of the double cone (10) is fixedly connected with the inner wall of the ash bucket through a connecting strip;

the steam humidification device is characterized by further comprising a heating device and a steam humidification pipeline, wherein the heating device is arranged on the outer peripheral surfaces of the upper barrel (13) and the middle cone (12);

the steam humidifying pipeline is connected with a steam humidifying and atomizing nozzle (3) through a steam valve (2), and the steam humidifying and atomizing nozzle (3) is arranged in the inlet pipe (4);

a temperature and humidity sensor (1) is fixedly arranged in the cylinder exhaust pipe, and the temperature and humidity sensor (1) and the steam valve (2) are arranged in a linkage mode.

2. The air dry dedusting device for the yellow phosphorus furnace according to claim 1, wherein the inclination angle of the inlet pipe (4) is α, and α is 10 to 16 °.

3. The dry dedusting apparatus for yellow phosphorus furnace gas according to claim 2, wherein the cross section of the inlet pipe (4) is rectangular, and the inlet pipe (4) has an inclination angle α satisfying tan α =0.5A/D, where a is the opening width of the inlet pipe (4) in the vertical direction, and D is the diameter of the upper cylinder (13).

4. The dry dedusting device for the yellow phosphorus furnace gas according to claim 2, further comprising a nitrogen gas inlet pipe, wherein the nitrogen gas inlet pipe is connected with a nitrogen gas nozzle (7) through a nitrogen gas valve (6), the nitrogen gas nozzle (7) is fixedly arranged in the ash discharge pipe, an oxygen content monitoring sensor (5) is fixedly arranged in the middle cone (12), and the oxygen content monitoring sensor (5) and the nitrogen gas nozzle (7) are arranged in a linkage manner.

5. The gas dry dedusting device for the yellow phosphorus furnace according to claim 4, characterized in that a material level meter (9) is arranged in the ash bucket, and the material level meter (9) is linked with the ash discharge valve (8).

6. The yellow phosphorus furnace gas dry dedusting device of claim 5, wherein the cylinder exhaust pipe is a gradually expanding cylinder exhaust pipe, and the expansion angle is 6-15 degrees.

7. The dry dedusting device for yellow phosphorus furnace gas according to any one of claims 1 to 6, wherein the heating device is a steam jacket (16) which is sleeved outside the upper cylinder (13) and the middle cone (12) and is communicated with each other, the upper part of the steam jacket (16) is provided with a steam inlet (15), and the lower part of the steam jacket (16) is provided with a condensed water outlet (11).

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